CN105111345A - Single-gas-phase fluidized bed discharge system applicable to multi-zone polymerization reaction as well as discharge method - Google Patents
Single-gas-phase fluidized bed discharge system applicable to multi-zone polymerization reaction as well as discharge method Download PDFInfo
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Abstract
The invention relates to a single-gas-phase fluidized bed discharge system applicable to a multi-zone polymerization reaction. The discharge system is arranged on a single-gas-phase fluidized bed reaction system and comprises a primary flash tank (2), a secondary flash tank (3) and a deactivating buffering bin (4), wherein a feed opening of the primary flash tank (2) is connected to a discharge opening of the single-gas-phase fluidized bed reaction system, the bottom of the primary flash tank (2) is connected to a feed opening of the secondary flash tank (3), the bottom of the secondary flash tank (3) is connected to the deactivating buffering bin (4), and tops of the primary flash tank (2) and the secondary flash tank (3) are both connected to the single-gas-phase fluidized bed reaction system. Compared with the prior art, the single-gas-phase fluidized bed discharge system applicable to the multi-zone polymerization reaction has the advantages of sufficient utilization of raw materials, low energy consumption, concise and smooth production process, high product quality and the like.
Description
Technical field
The present invention relates to a kind of single gas-phase fluidized-bed discharge system and discharging method, especially relate to a kind of gas-phase fluidized-bed discharge system of list and the discharging method that are applicable to multi-region polyreaction.
Background technology
Polyolefine is the maximum kind of world's general synthetic resin, and wherein polyvinyl resin estimates that the consumption in 2015 can reach 1,800 ten thousand tons, and expected capacity is at 1,600 ten thousand tons.The process modification of polyethylene production, the exploitation of innovation and new catalyzer is the focus of research at present.Poly production method can be divided into slurry process, solution method and vapor phase process according to medium in the 1980s.UCC (US5453471), BP (WO94/28032), Exxon (WO96/10591), by exploitation condensation and super condensation technology, overcome reactor and remove reaction heat difficulty and comonomer is selected and add-on the problem such as to be restricted and to make gas-phase fluidized bed Technology become the current polyethylene production process technology generally applied.
Gas-phase fluidized bed Technology is all generally carry out several steps such as raw material configuration, polyreaction, powder are degassed, granulation, conveying, packaging successively to carry out.Raw material layoutprocedure is all generally raw material is carried out to the activity that the process such as drying, deoxidation, removal of carbon monoxide prevent the impurity effect catalyzer in raw material.After polymerization procedure ethene, comonomer (butene-1 or hexene-1), iso-pentane (induced condensing agent) and hydrogen that mainly refinement treatment is crossed add fluidized-bed reactor, by the polyreaction that catalyzer injecting reactor carries out.The unstripped gas do not reacted is discharged from reactor head and is used through recycle gas compressor compression cycle.Reaction cycle gas makes the polyethylene powder fluidisation formed in reactor, and withdraws reaction heat by cycle condenser.In reactor, polyreaction proceeds to a certain degree, the resin generated is through Level control, directly be interrupted from reactor bottom (above grid distributor) and enter two design arrangement discharge system of 0.2 ~ 0.5 meter above reactor distributing plate, be then delivered to product degassing cabin by nitrogen or effluent gas recovery gas.The nitrogen passed into from the degassing cabin bottom hydrocarbon component carried resin powder is blown out by degassing cabin tower top and enters effluent gas recovery system, through filtration, cooling, condensation, foam removal, pressurization, cool again, after condensation again, again foam removal, reclaim the liquid materials such as corresponding comonomer, induced condensing agent, pumping meeting fluidized-bed reactor loop, non-condensable gases sends discharge system back to as delivering gas, or needs partial discharge torch because of pressure-controlling; Newly designed Sinopec ST technology, its flow process be this part gas again through membrane sepn facility, permeate step by step under elevated pressure, reclaim hydrocarbon gas to greatest extent.But facility investment is large, and step is many, flow process is longer, energy consumption is high, and not reduce from source and administer.
The powder of current application mode of discharging is all material from design arrangement 2 or 4 heavy caliber discharge gates discharges of 0.2 ~ 0.5 meter on grid distributor.Every 2 cover discharge systems are a pair, and large-scale reactor design two is to (4 discharge gates).In discharging process, resin powder (above grid distributor) bottom fluidized-bed reactor is discharged, and carried secretly and just entered reactor, the unstripped gas of also not participating in polyreaction and absorption in a large number and be dissolved in comonomer in resin and condensing agent, deliver into degassing cabin through gas.In degassing cabin, the gas carried secretly and the comonomer of vaporization and condensing agent are under heated nitrogen helps, effluent gas recovery system is entered with resin isolation, through filtering, cooling, freezing, foam removal, compression, cool again, more freezing, again after foam removal process, liquid is through pumped back reactor assembly, the delivering gas that major part noncondensable gas (mainly ethene, nitrogen, hydrogen) returns as discharge system is recycled, and small portion of gas is disposed to torch.
Structure design characteristic due to fluidized-bed reactor is reactor bottom charging, discharges, so namely powder discharge process has occurred that not participating in reaction mass is entrained with reactor by powder at bottom powder simultaneously.Do not participate in and react that the raw material that is discharged causes the loss of material, the consumption of energy increases, the problem of a series of increase production costs such as the processing load increasing of effluent gas recovery system.To be two covers blow by product discharge tank (PC) and product product blowdown system (PDS) intermittent type that tank (PBT) forms to another kind of powder discharge method carries out powder discharge.In alternate operating mode in parallel, implement gas conveying between the discharge system in every a pair PDS, to reduce the amount of monomer leaving reactive system.This kind of intermittent type discharging method can reduce to a certain extent carries waste problem secretly, but still there is the reduction of material, the energy and production efficiency or waste, the powder mobility of discharge is deteriorated and the problem such as degassed difficulty increasing.And because unreacted material is from leaving reactor, to the path length returned, reclaim the temperature of gas and pressure is repeated to be elevated for several times, the step of process is many, equipment is many, is easy to contaminated, usually occur the gas reclaimed, liquid discharge to the situation of torch.
Summary of the invention
Object of the present invention be exactly in order to overcome above-mentioned prior art exist defect and a kind of gas-phase fluidized-bed discharge system of list and the discharging method that are applicable to multi-region polyreaction are provided.
Object of the present invention can be achieved through the following technical solutions:
Be applicable to the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, this discharge system is arranged on single gas-phase fluidized-bed reactive system, it is characterized in that, described discharge system comprises primary flash tank, two-stage flash tank and deactivation surge bunker, described primary flash tank opening for feed is connected to single gas-phase fluidized-bed reactive system discharge gate, primary flash pot bottom is connected to two-stage flash tank opening for feed, two-stage flash pot bottom is connected to deactivation surge bunker, and described primary flash tank and two-stage flash tank top are all connected in the gas-phase fluidized-bed reactive system of described list.
The gas-phase fluidized-bed reactive system of described list comprises the recycle gas loop be made up of the gas-phase fluidized-bed reactor connected successively, recycle gas compressor and condenser, also comprise catalyst addition system, various raw materials system, described discharge gate is arranged on gas-phase fluidized-bed reactor.
Described primary flash tank and two-stage flash tank top are equipped with strainer, bottom is equipped with discharging surge tank, wherein strainer a in primary flash tank top is connected to described recycle gas compressor entrance by a centrifugal compressor, and primary flash pot bottom discharging surge tank a is arranged on primary flash pot bottom discharge gate and between two-stage flash tank opening for feed;
Two-stage flash tank top strainer b is connected to described centrifugal compressor and recovery system respectively, and two-stage flash pot bottom discharging surge tank b is connected to deactivation surge bunker.
Described strainer a, strainer b, discharging surge tank a and discharging surge tank b are provided with two.
Described discharge gate is provided with three layers, be respectively upper strata discharge gate, middle level discharge gate and lower floor's discharge gate, three layers of discharge gate are all pooled to the opening for feed of primary flash tank by pipeline and valve, each discharge gate is equipped with partition plunger valve, each plunger valve connects an electronic rotation valve, the speed of rotation of electronic rotation valve is controlled by setting material level, thus control withdrawal rate, compared with a large amount of liquid phases existed in the reactor bottom discharge of traditional design, arrange the unreacted liquid carried secretly in three layers of discharge gate discharge to reduce, so just can guarantee when load improves, ensure material fluidity, the burden of downstream recovery system is alleviated.Effectively can also save condensing agent simultaneously, increase its refrigerating efficiency.
Described upper strata discharge gate is positioned at 80% ~ 90% position of gas-phase fluidized-bed normal running charge level height, described middle level discharge gate is positioned at 40% ~ 60% position of gas-phase fluidized-bed normal running charge level normal running charge level height, 0.2 ~ 0.5m place above the grid distributor that described lower floor's discharge gate is arranged in reactor.
The discharge line of three layers of discharge gate connection and the sidewall of gas-phase fluidized-bed reactor are 45° angle, and described plunger valve is arranged in discharge line.
Be applicable to the discharging method of the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, it is characterized in that, the method comprises the following steps:
(1) unstripped gas is compressed through recycle gas compressor and after condenser condenses, is entered gas-phase fluidized-bed reactor from bottom and carries out polyreaction, the gas do not reacted is discharged from reactor head and is again entered the use of recycle gas compressor compression cycle, thus forming recycle gas loop, polymerisate is then discharged through reactor discharge gate;
(2) polymerisate that reactor discharge gate is discharged enters the flash distillation of primary flash tank, the nitrogen that flash tank tank deck steams, hydrogen, lighter hydrocarbons and part comonomer gas, after strainer a through primary flash tank top filters, part is discharged from strainer a top and enter recycle gas loop after centrifugal compressor supercharging, and rest part is discharged and entered two-stage flash tank together with the resin powder of discharging with primary flash pot bottom bottom strainer a;
(3) resin powder carries out secondary flash in two-stage flash tank, after two-stage flash tank tank deck steams the strainer b filtration of gas through top, easily solidifying class hydrocarbon gas enters recycle gas loop after centrifugal compressor supercharging, part non-condensable gases is expelled to recovery system, part non-condensable gases by discharge bottom strainer b and the bottom sending the discharging surge tank b of two-stage flash pot bottom back to as carrying gas, carry the resin powder that two-stage flash pot bottom discharges and be delivered to surge bunker together with supplying nitrogen;
(4) the resin powder that two-stage flash pot bottom is discharged enters surge bunker and continues separating impurity from top, gaseous impurities escapes and enter recovery system by surge bunker top filter, resin powder is postponed to rush bottom storehouse and is discharged, and namely obtains the resin powder product of finished product.
Part non-condensable gases is also had to enter surge bunker bottom in described step (3), at surge bunker) to be separated in resin powder after gaseous impurities, if resin powder needs to contact with air, then non-condensable gases is removed after water vapour humidification catalyzer and promotor residue in resin powder.
The operating pressure of gas-phase fluidized-bed reactor is 2.0 ~ 2.4MPa, and the operating pressure of primary flash tank is 0.7 ~ 1.6MPa, and the operating pressure of two-stage flash tank is 0.05 ~ 0.1MPa, and the operating pressure of deactivation surge bunker is 0.01 ~ 0.03MPa.
A non-condensable gases part can as delivering gas (nitrogen is gas as a supplement), enter two-stage flash tank and the resin powder of discharging bottom it is delivered to deactivation surge bunker, another part gas (nitrogen is gas as a supplement) is as the sweeping gas of deactivation surge bunker, enter from this middle and lower part, storehouse, assist comonomer residual in deresinate and condensing agent.Non-condensable gases is also as the blowback air of two-stage flash tank and deactivation surge bunker top filter.
In gas-phase fluidized-bed reactor, polymerisate is driven into primary flash tank by pressure drop, and does not need extra gas conveying, by often overlapping discharge system high frequency time, pulsed discharge, collecting continuous, the stable discharge stream of formation and entering surge bunker.Add designing from row function of discharge line like this, can prevent from remaining in the polymer melting plasticization in spool and drainage line.
The effect of primary flash tank removes polymerization product---the N in resin powder
2, H
2and whole or most in lighter hydrocarbons, after the strainer of a small amount of comonomer gas through primary flash tank top and centrifugal compressor supercharging, directly return reaction cycle gas return path; Resin powder after the flash distillation of primary flash surge tank, control and enter two-stage flash tank under pressure-controlling and under self gravitation effect to remove remaining a small amount of lighter hydrocarbons and most remainder hydrocarbon gas at charge level, after pressurization, directly return reaction cycle gas return path.
Resin powder after secondary flash is under the effect of carrying gas, be delivered to the deactivation surge bunker of large volume, continue remove the remaining hydro carbons of possibility and be hydrolyzed residual alkyl metal cpd, to guarantee the security of resin when subsequent touch air, from deactivation surge bunker top filter gas out, pressurize through effluent gas recovery system, cool freezing, the comonomer that further recovery is residual and condensing agent pumping returns reaction cycle gas return path, non-condensable gases (mainly nitrogen, containing a small amount of hydrogen and ethene) return as two-stage flash tank deck strainer b and the blowback air of deactivation surge bunker top strainer and the resin transfer gas of two-stage flash tank, the degassed medium of deactivation surge bunker and hydrolysis gas medium are by abundant recycle.
Compared with prior art, tool of the present invention has the following advantages:
(1) I and II successive flash vaporization is set to replace the pattern of original intersection discharging, step and the time of discharging can be greatly reduced, also become more convenient while ensureing yield, the gas flashed off is used after can also again reclaiming, and makes plant energy consumption become lower.
(2) because discharge gate, valve, pipeline are all than conventional small change, greatly reduce hardware facility and valve, structural requirement, cost of investment and running cost decline greatly; And without pulsating stress and surging force, reliability and the life-span of discharge system provide greatly.
(3) powder from fluidized-bed reactor through the process that I and II flash tank finally arrives surge bunker be with reactor between pressure reduction and powder self gravitation carry out for power, whole process is without the need to external impellent, the process entering surge bunker is blowed with traditional nitrogen, save nitrogen consumption and energy consumption, reduce the burden of effluent gas recovery system.
(4) in fluidized-bed reactor powder discharge the gas carried secretly can by hydrocarbon gas, N through primary flash
2, H
2enter in circulation gas etc. most gas through radial compressor compression, the operating pressure of primary flash tank and the operating pressure pressure reduction of gas-phase fluidized-bed reactor are little, can reduce compressor work, reduction energy consumption.Only have the gas of small part to enter effluent gas recovery system from top in two-stage flash tank and surge bunker, this process substantially reduces the path of discharge gas recovery walking, reduces the amount of effluent gas recovery process.
(5) directly can change recycle gas into participate in polyreaction and go after centrifugal compressor got back to by I and II flash drum overhead strainer, decrease difficulty and the load of follow-up effluent gas recovery process, reduce the loss of investment and running cost and material, save the energy consumption that material process needs, also stop the material pollution problem because Path too long causes.
(6) resin powder is at the surge bunker of large volume, can the remaining hydro carbons of effective elimination and the residual alkyl metal cpd of hydrolysis, ensure that the security of resin when subsequent touch air.
Accompanying drawing explanation
Fig. 1 is gas-phase fluidized-bed reactor discharge system process flow sheet of the present invention;
Fig. 2 is gas-phase fluidized-bed reactor structural representation of the present invention;
Fig. 3 is the discharge gate structural representation of gas-phase fluidized-bed reactor of the present invention.
In figure, 1 is gas-phase fluidized-bed reactor, and 2 is primary flash tank, and 3 is two-stage flash tank, 4 is deactivation surge bunker, and 5 is recycle gas compressor, and 6 is condenser, and 7 is strainer a, 8 is strainer b, and 9 is centrifugal compressor, and 10 is discharging surge tank a, and 11 is discharging surge tank b, 12 is upper strata discharge gate, and 13 is middle level discharge gate, and 14 is lower floor's discharge gate, 15 is grid distributor, and 16 is plunger valve, and 17 is electronic rotation valve, 18 is recovery system, and 19 is non-condensable gases, and 20 is water vapour.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
Comparative example
For the gas fluidized-bed process device of a set of annual output 300000 tons of LLDPE (LLDPE), its design loading is generally 37.5T/HR, produce conventional monomodal LLDPE film product, discharge per hour is about 25 times, fluidized-bed temperature in about 39 DEG C, dump temperature is about 60 ~ 65 DEG C.
Discharge system is arranged on single gas-phase fluidized-bed reactive system, the gas-phase fluidized-bed reactive system of described list comprises the recycle gas loop be made up of gas-phase fluidized-bed reactor 1 recycle gas compressor 5 connected successively and condenser 6, also comprise catalyst addition system, various raw materials system, the gas-liquid-solid concentration of gas-phase fluidized-bed reactor 1 inside as shown in Figure 2, from reactor lower part to reactor top, the concentration of unstripped gas reduces successively, part unstripped gas is at the bottom polymerization reaction take place of reactor, unreacted is polymerized particle completely and continues polymerization reaction take place with rising flow of feed gas on gas-phase fluidized-bed reactor 1 top, the unstripped gas that part does not react is discharged from fluidized-bed reactor top and is recycled together with unstripped gas and form recycle gas loop, described discharge gate is arranged on gas-phase fluidized-bed reactor 1, described discharge system comprises primary flash tank 2, two-stage flash tank 3 and deactivation surge bunker 4, described primary flash tank 2 opening for feed is connected to single gas-phase fluidized-bed reactive system discharge gate, two-stage flash tank 3 opening for feed is connected to bottom primary flash tank 2, deactivation surge bunker 4 is connected to bottom two-stage flash tank 3, described primary flash tank 2 and two-stage flash tank 3 top are all connected in the gas-phase fluidized-bed reactive system of described list.Described primary flash tank 2 and two-stage flash tank 3 top are equipped with strainer, bottom is equipped with discharging surge tank, wherein primary flash tank 2 top filter a7 is connected to described recycle gas compressor 5 entrance by a centrifugal compressor 9, and primary flash tank 2 bottom discharge surge tank a10 is arranged on primary flash tank 2 bottom discharging mouth and between two-stage flash tank 3 opening for feed; Two-stage flash tank 3 top filter b8 is connected to described centrifugal compressor 9 and recovery system 18 respectively, two-stage flash tank 3 bottom discharge surge tank b11 is connected to deactivation surge bunker 4, strainer a7, strainer b8, discharging surge tank a10 and discharging surge tank b11 are provided with two, so not only ensure that the efficient removal of discharging and carrying material in material secretly, also assures that the safe reliability of system, once somewhere fault, another path can be switched to immediately, ensure that the unimpeded, efficient of whole system.Wherein the material inlet of primary flash tank 2, two-stage flash tank 3, also can adopt tangential admission, reaches combination effect that cyclonic separation is separated with flash separation and strainer.
Traditional fluidized-bed reactor is for discharge port with the position of 0.3m above fluidized-bed bottom distance distribuor of fluidized bed.After polyreaction proceeds to a certain degree, discharge system just starts discharge.But because fluidized-bed reactor is bottom feed, be entrained out so the process that powder is discharged from bottom has a lot of materials when having neither part nor lot in reaction.Gas content in each discharge is about 35% ~ 38% (main component is ethene, hydrogen, nitrogen etc.), and liquid hydrocarbon (main component is comonomer and the cryogen) content of dissolving is about 200 ~ 250Kg/m
3.
Be applicable to the discharging method of the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, the method comprises the following steps:
(1) unstripped gas is compressed through recycle gas compressor 5 and after condenser 6 condensation, is entered gas-phase fluidized-bed reactor 1 from bottom and carries out polyreaction, the gas do not reacted is discharged from reactor head and is again entered the use of recycle gas compressor 5 compression cycle, thus forming recycle gas loop, polymerisate is then discharged through reactor discharge gate;
(2) polymerisate that reactor discharge gate is discharged enters primary flash tank 2 flash distillation, the nitrogen that flash tank tank deck steams, hydrogen, lighter hydrocarbons and part comonomer gas, after strainer a7 through primary flash tank 2 top filters, 27 ~ 28% from strainer a7 top discharge and after centrifugal compressor 9 supercharging, enter recycle gas loop, rest part is discharged and enter two-stage flash tank 3 together with the resin powder of discharging bottom primary flash tank 2 bottom strainer a7;
(3) resin powder carries out secondary flash in two-stage flash tank 3, after two-stage flash tank 3 tank deck steams the strainer b8 filtration of gas through top, easily solidifying class hydrocarbon gas enters recycle gas loop after centrifugal compressor 9 supercharging, 6 ~ 9% non-condensable gasess 19 are expelled to recovery system 18,1 ~ 2% non-condensable gases 19 by discharge bottom strainer b8 and the bottom sending the discharging surge tank b11 bottom two-stage flash tank 3 back to as carrying gas, carry the resin powder of discharging bottom two-stage flash tank 3 and be delivered to surge bunker 4 together with supplying nitrogen;
(4) the resin powder of discharging bottom two-stage flash tank 3 enters surge bunker 4 and continues separating impurity from top, gaseous impurities escapes and enter recovery system 18 by surge bunker 4 top filter, resin powder is postponed to rush bottom storehouse 4 and is discharged, and namely obtains the resin powder product of finished product.
In described step (3), part non-condensable gases 19 also enters surge bunker 4 bottom, to be separated in resin powder after gaseous impurities at surge bunker 4, if resin powder needs to contact with air, then non-condensable gases 19 is removed catalyzer and promotor residue in resin powder after water vapour 20 humidification.
Wherein the operating pressure of gas-phase fluidized-bed reactor 1 is 2.2MPa, and the operating pressure of primary flash tank 2 is 1.1MPa, and the operating pressure of two-stage flash tank 3 is 0.08MPa, and the operating pressure of deactivation surge bunker 4 is 0.02MPa.
Discharging process is through twice flash distillation, and make gas-entrainedly to enter reactor cycles gas process through very short path fast, the time is short, efficiency is high.It is more thorough that twice flash distillation makes gas be separated with powder simultaneously.The path of process is short, namely reduces elapsed time and the material loss of gas, achieves top efficiency, recycles the most efficiently.Even non-condensable gases (19), also can be fully utilized as the degassed medium of strainer blowback air and mass transport gas, deactivation surge bunker middle and lower part and hydrolysis medium.The required more traditional marker method of consumption supplementing nitrogen of system reduces by 80% ~ 85%.
Embodiment 1
For the gas fluidized-bed process device of a set of annual output 300000 tons of LLDPE (LLDPE), its design loading is generally 37.5T/HR, produce conventional monomodal LLDPE film product, discharge per hour is about 25 times, fluidized-bed temperature in about 39 DEG C, dump temperature is about 60 ~ 65 DEG C.The present invention is adopted to be applicable to the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, as shown in Figure 1, this discharge system is arranged on single gas-phase fluidized-bed reactive system, the gas-phase fluidized-bed reactive system of described list comprises the recycle gas loop be made up of gas-phase fluidized-bed reactor 1 recycle gas compressor 5 connected successively and condenser 6, also comprise catalyst addition system, various raw materials system, the gas-liquid-solid concentration of gas-phase fluidized-bed reactor 1 inside as shown in Figure 2, from reactor lower part to reactor top, the concentration of unstripped gas reduces successively, part unstripped gas is at the bottom polymerization reaction take place of reactor, unreacted is polymerized particle completely and continues polymerization reaction take place with rising flow of feed gas on gas-phase fluidized-bed reactor 1 top, the unstripped gas that part does not react is discharged from fluidized-bed reactor top and is recycled together with unstripped gas and form recycle gas loop, described discharge gate is arranged on gas-phase fluidized-bed reactor 1, described discharge system comprises primary flash tank 2, two-stage flash tank 3 and deactivation surge bunker 4, described primary flash tank 2 opening for feed is connected to single gas-phase fluidized-bed reactive system discharge gate, two-stage flash tank 3 opening for feed is connected to bottom primary flash tank 2, deactivation surge bunker 4 is connected to bottom two-stage flash tank 3, described primary flash tank 2 and two-stage flash tank 3 top are all connected in the gas-phase fluidized-bed reactive system of described list.Described primary flash tank 2 and two-stage flash tank 3 top are equipped with strainer, bottom is equipped with discharging surge tank, wherein primary flash tank 2 top filter a7 is connected to described recycle gas compressor 5 entrance by a centrifugal compressor 9, and primary flash tank 2 bottom discharge surge tank a10 is arranged on primary flash tank 2 bottom discharging mouth and between two-stage flash tank 3 opening for feed; Two-stage flash tank 3 top filter b8 is connected to described centrifugal compressor 9 and recovery system 18 respectively, two-stage flash tank 3 bottom discharge surge tank b11 is connected to deactivation surge bunker 4, strainer a7, strainer b8, discharging surge tank a10 and discharging surge tank b11 are provided with two, so not only ensure that the efficient removal of discharging and carrying material in material secretly, also assures that the safe reliability of system, once somewhere fault, another path can be switched to immediately, ensure that the unimpeded, efficient of whole system.Wherein the material inlet of primary flash tank 2, two-stage flash tank 3, also can adopt tangential admission, reaches combination effect that cyclonic separation is separated with flash separation and strainer.
As shown in Figure 3, described discharge gate is provided with three layers, be respectively upper strata discharge gate 12, middle level discharge gate 13 and lower floor's discharge gate 14, three layers of discharge gate are all pooled to the opening for feed of primary flash tank 2 by pipeline and valve, each discharge gate is equipped with partition plunger valve 16, each plunger valve 16 connects an electronic rotation valve 17, is controlled the speed of rotation of electronic rotation valve 17, thus control withdrawal rate by setting material level.Described upper strata discharge gate 12 is positioned at 80% position of gas-phase fluidized-bed normal running charge level height, described middle level discharge gate 13 is positioned at 40% position of gas-phase fluidized-bed normal running charge level normal running charge level height, 0.2m place above the grid distributor 15 that described lower floor's discharge gate 14 is arranged in reactor.The discharge line of three layers of discharge gate connection and the sidewall of gas-phase fluidized-bed reactor 1 are 60 ° of angles, and described plunger valve 16 is arranged in discharge line.After adopting this discharge gate, the gas content in each discharge is about 18% ~ 25% (main component is ethene, hydrogen, nitrogen etc.), and liquid hydrocarbon (main component is comonomer and the cryogen) content of dissolving is about 150 ~ 200Kg/m
3.
Be applicable to the discharging method of the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, the method comprises the following steps:
(1) unstripped gas is compressed through recycle gas compressor 5 and after condenser 6 condensation, is entered gas-phase fluidized-bed reactor 1 from bottom and carries out polyreaction, the gas do not reacted is discharged from reactor head and is again entered the use of recycle gas compressor 5 compression cycle, thus forming recycle gas loop, polymerisate is then discharged through reactor discharge gate;
(2) polymerisate that reactor discharge gate is discharged enters primary flash tank 2 flash distillation, the nitrogen that flash tank tank deck steams, hydrogen, lighter hydrocarbons and part comonomer gas, after strainer a7 through primary flash tank 2 top filters, 14% from strainer a7 top discharge and after centrifugal compressor 9 supercharging, enter recycle gas loop, rest part is discharged and enter two-stage flash tank 3 together with the resin powder of discharging bottom primary flash tank 2 bottom strainer a7;
(3) resin powder carries out secondary flash in two-stage flash tank 3, after two-stage flash tank 3 tank deck steams the strainer b8 filtration of gas through top, easily solidifying class hydrocarbon gas enters recycle gas loop after centrifugal compressor 9 supercharging, 4% non-condensable gases 19 is expelled to recovery system 18,1% non-condensable gases 19 by discharge bottom strainer b8 and the bottom sending the discharging surge tank b11 bottom two-stage flash tank 3 back to as carrying gas, carry the resin powder of discharging bottom two-stage flash tank 3 and be delivered to surge bunker 4 together with supplying nitrogen;
(4) the resin powder of discharging bottom two-stage flash tank 3 enters surge bunker 4 and continues separating impurity from top, gaseous impurities escapes and enter recovery system 18 by surge bunker 4 top filter, resin powder is postponed to rush bottom storehouse 4 and is discharged, and namely obtains the resin powder product of finished product.
In described step (3), part non-condensable gases 19 also enters surge bunker 4 bottom, to be separated in resin powder after gaseous impurities at surge bunker 4, if resin powder needs to contact with air, then non-condensable gases 19 is removed catalyzer and promotor residue in resin powder after water vapour 20 humidification.
Wherein the operating pressure of gas-phase fluidized-bed reactor 1 is 2.0MPa, and the operating pressure of primary flash tank 2 is 0.7, and the operating pressure of two-stage flash tank 3 is 0.05, and the operating pressure of deactivation surge bunker 4 is 0.01.
Discharging process makes gas-entrainedly to enter circulation gas process through short path fast through twice flash distillation, and it is more thorough that twice flash distillation makes gas be separated with powder simultaneously.The path of process is short, namely reduces material loss more than 80%, and energy consumption reduces by 65%.The required more traditional marker method of consumption supplementing supplying nitrogen of simultaneity factor reduces by 80%.And the contaminated probability of quality of the gas reclaimed, liquid and non-condensable gases reduces greatly.The present invention is in line with the thinking from watershed management, have raw material and energy utilization fully, succinct smooth, the advantage such as equipment simplifies miniaturization, the short contaminated possibility in material path is little, quality product is high, the fast Transition Materials of production interchange is few of low, the Production Flow Chart of device material consumption, this invention is also applicable for the fluidized-bed reactor of traditional design and operational stage.
Embodiment 2
For the gas fluidized-bed process device of a set of annual output 300000 tons of LLDPE (LLDPE), its design loading is generally 37.5T/HR, produce conventional monomodal LLDPE film product, discharge per hour is about 25 times, fluidized-bed temperature in about 39 DEG C, dump temperature is about 60 ~ 65 DEG C.The present invention is adopted to be applicable to the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, as shown in Figure 1, this discharge system is arranged on single gas-phase fluidized-bed reactive system, the gas-phase fluidized-bed reactive system of described list comprises the recycle gas loop be made up of gas-phase fluidized-bed reactor 1 recycle gas compressor 5 connected successively and condenser 6, also comprise catalyst addition system, various raw materials system, the gas-liquid-solid concentration of gas-phase fluidized-bed reactor 1 inside as shown in Figure 2, from reactor lower part to reactor top, the concentration of unstripped gas reduces successively, part unstripped gas is at the bottom polymerization reaction take place of reactor, unreacted is polymerized particle completely and continues polymerization reaction take place with rising flow of feed gas on gas-phase fluidized-bed reactor 1 top, the unstripped gas that part does not react is discharged from fluidized-bed reactor top and is recycled together with unstripped gas and form recycle gas loop, described discharge gate is arranged on gas-phase fluidized-bed reactor 1, described discharge system comprises primary flash tank 2, two-stage flash tank 3 and deactivation surge bunker 4, described primary flash tank 2 opening for feed is connected to single gas-phase fluidized-bed reactive system discharge gate, two-stage flash tank 3 opening for feed is connected to bottom primary flash tank 2, deactivation surge bunker 4 is connected to bottom two-stage flash tank 3, described primary flash tank 2 and two-stage flash tank 3 top are all connected in the gas-phase fluidized-bed reactive system of described list.Described primary flash tank 2 and two-stage flash tank 3 top are equipped with strainer, bottom is equipped with discharging surge tank, wherein primary flash tank 2 top filter a7 is connected to described recycle gas compressor 5 entrance by a centrifugal compressor 9, and primary flash tank 2 bottom discharge surge tank a10 is arranged on primary flash tank 2 bottom discharging mouth and between two-stage flash tank 3 opening for feed; Two-stage flash tank 3 top filter b8 is connected to described centrifugal compressor 9 and recovery system 18 respectively, two-stage flash tank 3 bottom discharge surge tank b11 is connected to deactivation surge bunker 4, strainer a7, strainer b8, discharging surge tank a10 and discharging surge tank b11 are provided with two, so not only ensure that the efficient removal of discharging and carrying material in material secretly, also assures that the safe reliability of system, once somewhere fault, another path can be switched to immediately, ensure that the unimpeded, efficient of whole system.Wherein the material inlet of primary flash tank 2, two-stage flash tank 3, also can adopt tangential admission, reaches combination effect that cyclonic separation is separated with flash separation and strainer.
As shown in Figure 3, described discharge gate is provided with three layers, be respectively upper strata discharge gate 12, middle level discharge gate 13 and lower floor's discharge gate 14, three layers of discharge gate are all pooled to the opening for feed of primary flash tank 2 by pipeline and valve, each discharge gate is equipped with partition plunger valve 16, each plunger valve 16 connects an electronic rotation valve 17, is controlled the speed of rotation of electronic rotation valve 17, thus control withdrawal rate by setting material level.Described upper strata discharge gate 12 is positioned at 90% position of gas-phase fluidized-bed normal running charge level height, described middle level discharge gate 13 is positioned at 60% position of gas-phase fluidized-bed normal running charge level normal running charge level height, 0.5m place above the grid distributor 15 that described lower floor's discharge gate 14 is arranged in reactor.The discharge line of three layers of discharge gate connection and the sidewall of gas-phase fluidized-bed reactor 1 are 60 ° of angles, and described plunger valve 16 is arranged in discharge line.
Be applicable to the discharging method of the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, the method comprises the following steps:
(1) unstripped gas is compressed through recycle gas compressor 5 and after condenser 6 condensation, is entered gas-phase fluidized-bed reactor 1 from bottom and carries out polyreaction, the gas do not reacted is discharged from reactor head and is again entered the use of recycle gas compressor 5 compression cycle, thus forming recycle gas loop, polymerisate is then discharged through reactor discharge gate;
(2) polymerisate that reactor discharge gate is discharged enters primary flash tank 2 flash distillation, the nitrogen that flash tank tank deck steams, hydrogen, lighter hydrocarbons and part comonomer gas, after strainer a7 through primary flash tank 2 top filters, 17% from strainer a7 top discharge and after centrifugal compressor 9 supercharging, enter recycle gas loop, rest part is discharged and enter two-stage flash tank 3 together with the resin powder of discharging bottom primary flash tank 2 bottom strainer a7;
(3) resin powder carries out secondary flash in two-stage flash tank 3, after two-stage flash tank 3 tank deck steams the strainer b8 filtration of gas through top, easily solidifying class hydrocarbon gas enters recycle gas loop after centrifugal compressor 9 supercharging, 8% non-condensable gases 19 is expelled to recovery system 18,2% non-condensable gases 19 by discharge bottom strainer b8 and the bottom sending the discharging surge tank b11 bottom two-stage flash tank 3 back to as carrying gas, carry the resin powder of discharging bottom two-stage flash tank 3 and be delivered to surge bunker 4 together with supplying nitrogen;
(4) the resin powder of discharging bottom two-stage flash tank 3 enters surge bunker 4 and continues separating impurity from top, gaseous impurities escapes and enter recovery system 18 by surge bunker 4 top filter, resin powder is postponed to rush bottom storehouse 4 and is discharged, and namely obtains the resin powder product of finished product.
In described step (3), part non-condensable gases 19 also enters surge bunker 4 bottom, to be separated in resin powder after gaseous impurities at surge bunker 4, if resin powder needs to contact with air, then non-condensable gases 19 is removed catalyzer and promotor residue in resin powder after water vapour 20 humidification.
Wherein the operating pressure of gas-phase fluidized-bed reactor 1 is 2.4MPa, and the operating pressure of primary flash tank 2 is 1.6MPa, and the operating pressure of two-stage flash tank 3 is 0.1MPa, and the operating pressure of deactivation surge bunker 4 is 0.03MPa.
Discharging process makes gas-entrainedly to enter circulation gas process through short path fast through twice flash distillation, and it is more thorough that twice flash distillation makes gas be separated with powder simultaneously.The path of process is short, namely reduces material loss more than 80%, and energy consumption reduces by 70%.The required more traditional marker method of consumption supplementing supplying nitrogen of simultaneity factor reduces by 92%.And the contaminated probability of quality of the gas reclaimed, liquid and non-condensable gases reduces greatly.The present invention is in line with the thinking from watershed management, have raw material and energy utilization fully, succinct smooth, the advantage such as equipment simplifies miniaturization, the short contaminated possibility in material path is little, quality product is high, the fast Transition Materials of production interchange is few of low, the Production Flow Chart of device material consumption, this invention is also applicable for the fluidized-bed reactor of traditional design and operational stage.
Embodiment 3
For the gas fluidized-bed process device of a set of annual output 300000 tons of LLDPE (LLDPE), its design loading is generally 37.5T/HR, produce conventional monomodal LLDPE film product, discharge per hour is about 25 times, fluidized-bed temperature in about 39 DEG C, dump temperature is about 60 ~ 65 DEG C.The present invention is adopted to be applicable to the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, as shown in Figure 1, this discharge system is arranged on single gas-phase fluidized-bed reactive system, the gas-phase fluidized-bed reactive system of described list comprises the recycle gas loop be made up of gas-phase fluidized-bed reactor 1 recycle gas compressor 5 connected successively and condenser 6, also comprise catalyst addition system, various raw materials system, the gas-liquid-solid concentration of gas-phase fluidized-bed reactor 1 inside as shown in Figure 2, from reactor lower part to reactor top, the concentration of unstripped gas reduces successively, part unstripped gas is at the bottom polymerization reaction take place of reactor, unreacted is polymerized particle completely and continues polymerization reaction take place with rising flow of feed gas on gas-phase fluidized-bed reactor 1 top, the unstripped gas that part does not react is discharged from fluidized-bed reactor top and is recycled together with unstripped gas and form recycle gas loop, described discharge gate is arranged on gas-phase fluidized-bed reactor 1, described discharge system comprises primary flash tank 2, two-stage flash tank 3 and deactivation surge bunker 4, described primary flash tank 2 opening for feed is connected to single gas-phase fluidized-bed reactive system discharge gate, two-stage flash tank 3 opening for feed is connected to bottom primary flash tank 2, deactivation surge bunker 4 is connected to bottom two-stage flash tank 3, described primary flash tank 2 and two-stage flash tank 3 top are all connected in the gas-phase fluidized-bed reactive system of described list.Described primary flash tank 2 and two-stage flash tank 3 top are equipped with strainer, bottom is equipped with discharging surge tank, wherein primary flash tank 2 top filter a7 is connected to described recycle gas compressor 5 entrance by a centrifugal compressor 9, and primary flash tank 2 bottom discharge surge tank a10 is arranged on primary flash tank 2 bottom discharging mouth and between two-stage flash tank 3 opening for feed; Two-stage flash tank 3 top filter b8 is connected to described centrifugal compressor 9 and recovery system 18 respectively, two-stage flash tank 3 bottom discharge surge tank b11 is connected to deactivation surge bunker 4, strainer a7, strainer b8, discharging surge tank a10 and discharging surge tank b11 are provided with two, so not only ensure that the efficient removal of discharging and carrying material in material secretly, also assures that the safe reliability of system, once somewhere fault, another path can be switched to immediately, ensure that the unimpeded, efficient of whole system.Wherein the material inlet of primary flash tank 2, two-stage flash tank 3, also can adopt tangential admission, reaches combination effect that cyclonic separation is separated with flash separation and strainer.
As shown in Figure 3, described discharge gate is provided with three layers, be respectively upper strata discharge gate 12, middle level discharge gate 13 and lower floor's discharge gate 14, three layers of discharge gate are all pooled to the opening for feed of primary flash tank 2 by pipeline and valve, each discharge gate is equipped with partition plunger valve 16, each plunger valve 16 connects an electronic rotation valve 17, is controlled the speed of rotation of electronic rotation valve 17, thus control withdrawal rate by setting material level.Described upper strata discharge gate 12 is positioned at 85% position of gas-phase fluidized-bed normal running charge level height, described middle level discharge gate 13 is positioned at 50% position of gas-phase fluidized-bed normal running charge level normal running charge level height, 0.35m place above the grid distributor 15 that described lower floor's discharge gate 14 is arranged in reactor.The discharge line of three layers of discharge gate connection and the sidewall of gas-phase fluidized-bed reactor 1 are 60 ° of angles, and described plunger valve 16 is arranged in discharge line.
Be applicable to the discharging method of the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, the method comprises the following steps:
(1) unstripped gas is compressed through recycle gas compressor 5 and after condenser 6 condensation, is entered gas-phase fluidized-bed reactor 1 from bottom and carries out polyreaction, the gas do not reacted is discharged from reactor head and is again entered the use of recycle gas compressor 5 compression cycle, thus forming recycle gas loop, polymerisate is then discharged through reactor discharge gate;
(2) polymerisate that reactor discharge gate is discharged enters primary flash tank 2 flash distillation, the nitrogen that flash tank tank deck steams, hydrogen, lighter hydrocarbons and part comonomer gas, after strainer a7 through primary flash tank 2 top filters, 16% gas is discharged from strainer a7 top and enter recycle gas loop after centrifugal compressor 9 supercharging, and rest part is discharged and enter two-stage flash tank 3 together with the resin powder of discharging bottom primary flash tank 2 bottom strainer a7;
(3) resin powder carries out secondary flash in two-stage flash tank 3, after two-stage flash tank 3 tank deck steams the strainer b8 filtration of gas through top, easily solidifying class hydrocarbon gas enters recycle gas loop after centrifugal compressor 9 supercharging, 6% non-condensable gases 19 is expelled to recovery system 18,2% non-condensable gases 19 by discharge bottom strainer b8 and the bottom sending the discharging surge tank b11 bottom two-stage flash tank 3 back to as carrying gas, carry the resin powder of discharging bottom two-stage flash tank 3 and be delivered to surge bunker 4 together with supplying nitrogen;
(4) the resin powder of discharging bottom two-stage flash tank 3 enters surge bunker 4 and continues separating impurity from top, gaseous impurities escapes and enter recovery system 18 by surge bunker 4 top filter, resin powder is postponed to rush bottom storehouse 4 and is discharged, and namely obtains the resin powder product of finished product.
In described step (3), part non-condensable gases 19 also enters surge bunker 4 bottom, to be separated in resin powder after gaseous impurities at surge bunker 4, if resin powder needs to contact with air, then non-condensable gases 19 is removed catalyzer and promotor residue in resin powder after water vapour 20 humidification.
Wherein the operating pressure of gas-phase fluidized-bed reactor 1 is 2.2MPa, and the operating pressure of primary flash tank 2 is 1.1MPa, and the operating pressure of two-stage flash tank 3 is 0.08MPa, and the operating pressure of deactivation surge bunker 4 is 0.02MPa.
Discharging process makes gas-entrainedly to enter circulation gas process through short path fast through twice flash distillation, and it is more thorough that twice flash distillation makes gas be separated with powder simultaneously.The path of process is short, namely reduces material loss more than 80%, and energy consumption reduces by 68%.The required more traditional marker method of consumption supplementing supplying nitrogen of simultaneity factor reduces by 86%.And the contaminated probability of quality of the gas reclaimed, liquid and non-condensable gases reduces greatly.The present invention is in line with the thinking from watershed management, have raw material and energy utilization fully, succinct smooth, the advantage such as equipment simplifies miniaturization, the short contaminated possibility in material path is little, quality product is high, the fast Transition Materials of production interchange is few of low, the Production Flow Chart of device material consumption, this invention is also applicable for the fluidized-bed reactor of traditional design and operational stage.
Claims (10)
1. be applicable to the gas-phase fluidized-bed discharge system of list of multi-region polyreaction, this discharge system is arranged on single gas-phase fluidized-bed reactive system, it is characterized in that, described discharge system comprises primary flash tank (2), two-stage flash tank (3) and deactivation surge bunker (4), described primary flash tank (2) opening for feed is connected to single gas-phase fluidized-bed reactive system discharge gate, primary flash tank (2) bottom is connected to two-stage flash tank (3) opening for feed, two-stage flash tank (3) bottom is connected to deactivation surge bunker (4), described primary flash tank (2) and two-stage flash tank (3) top are all connected in the gas-phase fluidized-bed reactive system of described list.
2. the gas-phase fluidized-bed discharge system of list being applicable to multi-region polyreaction according to claim 1, it is characterized in that, the gas-phase fluidized-bed reactive system of described list comprises the recycle gas loop be made up of the gas-phase fluidized-bed reactor connected successively (1), recycle gas compressor (5) and condenser (6), also comprise catalyst addition system, various raw materials system, described discharge gate is arranged on gas-phase fluidized-bed reactor (1).
3. the gas-phase fluidized-bed discharge system of list being applicable to multi-region polyreaction according to claim 2, it is characterized in that, described primary flash tank (2) and two-stage flash tank (3) top are equipped with strainer, bottom is equipped with discharging surge tank, wherein primary flash tank (2) top filter a (7) is connected to described recycle gas compressor (5) entrance by a centrifugal compressor (9), primary flash tank (2) bottom discharge surge tank a (10) is arranged on primary flash tank (2) bottom discharging mouth and between two-stage flash tank (3) opening for feed,
Two-stage flash tank (3) top filter b (8) is connected to described centrifugal compressor (9) and recovery system (18) respectively, and two-stage flash tank (3) bottom discharge surge tank b (11) is connected to deactivation surge bunker (4).
4. the gas-phase fluidized-bed discharge system of list being applicable to multi-region polyreaction according to claim 3, it is characterized in that, described strainer a (7), strainer b (8), discharging surge tank a (10) and discharging surge tank b (11) are provided with two.
5. the gas-phase fluidized-bed discharge system of list being applicable to multi-region polyreaction according to claim 2, it is characterized in that, described discharge gate is provided with three layers, be respectively upper strata discharge gate (12), middle level discharge gate (13) and lower floor's discharge gate (14), three layers of discharge gate are all pooled to the opening for feed of primary flash tank (2) by pipeline and valve, each discharge gate is equipped with partition plunger valve (16), each plunger valve (16) connects an electronic rotation valve (17), the speed of rotation of electronic rotation valve (17) is controlled by setting material level, thus control withdrawal rate.
6. the gas-phase fluidized-bed discharge system of list being applicable to multi-region polyreaction according to claim 5, it is characterized in that, described upper strata discharge gate (12) is positioned at 80% ~ 90% position of gas-phase fluidized-bed normal running charge level height, described middle level discharge gate (13) is positioned at 40% ~ 60% position of gas-phase fluidized-bed normal running charge level normal running charge level height, and described lower floor's discharge gate (14) is arranged in 0.2 ~ 0.5m place, grid distributor (15) top of reactor.
7. the gas-phase fluidized-bed discharge system of list being applicable to multi-region polyreaction according to claim 5, it is characterized in that, the discharge line of three layers of discharge gate connection and the sidewall of gas-phase fluidized-bed reactor (1) are 60 ° of angles, and described plunger valve (16) is arranged in discharge line.
8. a discharging method for the gas-phase fluidized-bed discharge system of the list being applicable to multi-region polyreaction as described in as arbitrary in claim 1 ~ 7, it is characterized in that, the method comprises the following steps:
(1) unstripped gas is compressed through recycle gas compressor (5) and after condenser (6) condensation, is entered gas-phase fluidized-bed reactor (1) from bottom and carries out polyreaction, the gas do not reacted is discharged from reactor head and is again entered the use of recycle gas compressor (5) compression cycle, thus forming recycle gas loop, polymerisate is then discharged through reactor discharge gate;
(2) polymerisate that reactor discharge gate is discharged enters primary flash tank (2) flash distillation, the nitrogen that flash tank tank deck steams, hydrogen, lighter hydrocarbons and part comonomer gas, after strainer a (7) through primary flash tank (2) top filters, part is discharged from strainer a (7) top and enter recycle gas loop after centrifugal compressor (9) supercharging, and rest part is discharged from strainer a (7) bottom and entered two-stage flash tank (3) together with the resin powder of discharging with primary flash tank (2) bottom;
(3) resin powder carries out secondary flash in two-stage flash tank (3), after two-stage flash tank (3) tank deck steams strainer b (8) filtration of gas through top, easily solidifying class hydrocarbon gas enters recycle gas loop after centrifugal compressor (9) supercharging, part non-condensable gases (19) is expelled to recovery system (18), part non-condensable gases (19) is discharged by strainer b (8) bottom and the bottom sending the discharging surge tank b (11) bottom two-stage flash tank (3) back to as carrying gas, carry the resin powder of discharging two-stage flash tank (3) bottom and be delivered to surge bunker (4) together with supplying nitrogen,
(4) the resin powder that two-stage flash tank (3) bottom is discharged enters surge bunker (4) and continues separating impurity from top, gaseous impurities escapes and enter recovery system (18) by surge bunker (4) top filter, resin powder is postponed and is rushed the discharge of bottom, storehouse (4), namely obtains the resin powder product of finished product.
9. the discharging method being applicable to the gas-phase fluidized-bed discharge system of list of multi-region polyreaction according to claim 8, it is characterized in that, part non-condensable gases (19) is also had to enter surge bunker (4) bottom in described step (3), to be separated in resin powder after gaseous impurities at surge bunker (4), if resin powder needs to contact with air, then non-condensable gases (19) is removed catalyzer and promotor residue in resin powder after water vapour (20) humidification.
10. the method for the discharge of the gas-phase fluidized-bed discharge system of the list being applicable to multi-region polyreaction according to claim 8 or claim 9, it is characterized in that, the operating pressure of gas-phase fluidized-bed reactor (1) is 2.0 ~ 2.4MPa, the operating pressure of primary flash tank (2) is 0.7 ~ 1.6MPa, the operating pressure of two-stage flash tank (3) is 0.05 ~ 0.1MPa, and the operating pressure of deactivation surge bunker (4) is 0.01 ~ 0.03MPa.
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